Process for electrolytic production of aluminum

ABSTRACT

A new method for the electrolytic production of aluminum, using a new electrolyte composition and low temperature operation, is provided. The electrolyte comprises a mixture of aluminum fluoride-potassium fluoride with from about 2 wt. % to 6 wt. % of alumina. The new electrolyte allows for the electrolytical reduction of alumina at temperatures as low as 700° C. The lower temperature allows for the use of inert anodes, and is conducive to the use of wetted cathodes. The new electrolyte mixture has a higher solubility for alumina and remains entirely liquid, even with 5 wt. % of alumina present in the electrolyte during electrolysis. Oxygen (O 2 ) is the only gas generated during alumina electrolysis with the new electrolyte and the inert anodes, thus eliminating the production of greenhouse gases. Anodes and cathodes can be mounted in either a vertical, horizontal, or some other configuration.

CONTRACTUAL ORIGIN OF INVENTION

The United States Government has rights in this invention pursuant to Contract No. W-31-109-ENG-38 between the U.S. Department of Energy and the University of Chicago, representing Argonne National Laboratory.

BACKGROUND OF THE INVENTION

1. Field of the Invention

This invention relates to an electrolyte and a method for producing aluminum at lower temperatures, and, more specifically, this invention relates to an electrolyte that enables a method for producing aluminum at lower temperatures using a myriad of electrodes, including inert anodes and wettable cathodes.

2. Background of the Invention

Primary aluminum is produced by the electrolysis of alumina in a cell (or pot) containing a molten fluoride salt based on the AlF₃—NaF system. During electrolysis, carbon dioxide gas forms at the anode and escapes from the cell, while liquid aluminum metal forms at the cathode at the bottom of the cell. The electrolytic process (called the Hall-Héroult process) operates at temperatures in excess of 900° C. Such high temperatures are detrimental for a number of reasons, including deterioration of cell components.

Another drawback to typical aluminum production processes is the use of consumable carbon anode materials. The gradual consumption of the carbon anodes, due to reaction of the carbon with oxygen forming carbon dioxide gas bubbles at the anode surface, necessitates constant repositioning of the remaining anode with the cathode to maintain an optimal anode-to-cathode distance. Ultimately, the anodes must be replaced. Also, the manufacture and use of carbon anodes contributes to the production of greenhouse gases such as carbon dioxide and perfluorocarbons (PFCs).

The aluminum community has long-searched for a so-called inert anode (one that is not consumed by the electrolysis process) for use in aluminum production cells to replace consumable carbon anodes. This research has spanned several decades. All of the so-called inert anode materials characterized to date have had various shortcomings with respect to attributes needed for commercial success. Anodes made of ceramic or cermet materials cause some practical engineering problems, such as poor thermal shock resistance, electrical connection, operational challenges and scalability etc. Anodes made of metal have the potential advantage of improved electrical and mechanical performance over cermet or ceramic materials. However, work on metal anodes at high temperatures (i.e., between 900° C. and 1000° C.) has had only limited success.

Low temperature electrolytes, those that remain liquid below 800° C., can increase the utility of inert anodes. Recent work in this area has mainly focused on the sodium fluoride (NaF)—aluminum fluoride (AlF₃)-based electrolyte system, i.e. so called low bath ratio (NaF/AlF₃) melts. Due to a relatively low solubility of alumina (Al₂O₃) in these low-temperature (around 750° C.) electrolytes, a slurry-cell concept was proposed to keep solid alumina in suspension during electrolysis, allowing the alumina activity in the electrolyte to remain high during electrolysis. However, slurry-cell operation causes operational difficulties and problems with metal collection, as well as the fact that very strict requirements on cell design are needed to maintain the alumina in suspension.

Another drawback to typical aluminum production processes is the need to maintain a sufficient molten aluminum metal pool at the bottom of the cell. Significant operation difficulties occur when the carbon blocks on the cell bottom are exposed to the molten salt electrolyte bath. Since molten aluminum does not wet carbon, a significant quantity of aluminum is required to totally cover the cell bottom. The presence of this deep aluminum pool leads to process inefficiencies due to fluctuations at the bath-aluminum interface resulting from magnetic fields generated in the metal pool during electrolysis. These fluctuations are minimized with the use of so-called wetted cathodes, i.e., cathode substrate materials that are wet by molten aluminum.

Still another drawback to typical aluminum production is the large dimensions or “footprint” of the typical alumina electrolytic cell. This is due to the horizontal alignment of the electrodes, necessitated by the lack of suitable inert anodes and wetted cathodes required to maintain a stable anode-to-cathode distance in cells with vertically aligned electrodes.

A need exists in the art for an electrolytic method for aluminum production that operates in low-temperature electrolytes, i.e., one with an operating temperature less than 800° C. The method should eliminate the need for consumable carbon anodes and allow for the use of inert anodes, wetted cathodes, and/or bi-polar electrodes in horizontal, vertical, or other arrangement. The method should also provide for a constant distance between anode and cathode during the electrolysis of alumina to provide an electrically stable electrolysis environment. In addition, the method should provide an electrolyte which is entirely liquid at the operating temperature.

SUMMARY OF INVENTION

An object of the present invention is to provide a method of alumina electrolysis that overcomes many of the disadvantages of the prior art.

Another object of the present invention is to electrolyze alumina to aluminum at temperatures lower than 800° C. A feature of the invention is an electrolyte salt bath based on a mixture of aluminum fluoride (AlF₃)—potassium fluoride (KF) containing alumina (Al₂O₃) for aluminum production by electrolysis. An advantage of this invention is that it allows for the electrolytic production of aluminum at lower temperatures, and thus lowers costs including capital, operational, and environmental costs.

Still another object of the present invention is to provide an electrolyte whereby the electrolyte is stable during electrolysis operations. A feature of the invention is an electrolyte which has a relatively low vapor pressure (less than 10 millibar) in the process range temperature of between 660° C. and 1000° C. An advantage of this feature is that the concentrations of the electrolyte's components remain relatively constant during electrolysis.

Yet another object of the present invention is to provide an electrolyte which maintains a liquid phase during electrolysis operations. A feature of the invention is an electrolyte which has higher alumina solubility than in currently used low-temperature electrolytes. An advantage of this feature is that cell design and operation requirements become more flexible.

Still another object of the present invention is to provide a method whereby inert anodes can be used. A feature of the invention is that a lower operational temperature and electrolyte composition allows for the use of a greater selection of inert anode materials. An advantage of this feature is that the inert anode is not consumed by the electrolytic process. An additional advantage is a significant lowering of costs.

Yet another object of the invention is to provide a low temperature metal production method which uses wetted cathodes. A feature of the invention is that wetted cathodes require only a thin film of molten aluminum on their surface. An advantage of this feature is that fluctuations at the bath aluminum interface resulting from magnetic fields generated in the molten aluminum are minimized, allowing a lower anode-cathode distance that results in a lower cell voltage. Another advantage is that the aluminum film protects the cathode surface from the bath. Yet another advantage is the minimization or prevention of fine aluminum droplets that may become unattached from a cathode that is not wetted, resulting in process inefficiencies due to back reaction at the anode. An additional advantage is further cost savings.

Still another object of the invention is to provide a metal production method which can use vertical or slanted inert anodes, and vertical or slanted wetted cathodes. A feature of this invention is a decrease in the footprint of the electrolytic cell for a given production rate. An advantage of this feature is easier energy management of the electrolytic process. A smaller electrolytic cell both needs less heat input and has a lesser heat loss due to a smaller surface area and less heat radiation. Since less heat input is required, an additional advantage is that a lower current density (CD) can be used further reducing cell voltage. This feature thus gives additional savings.

Yet another object of the present invention is to provide a method whereby the distance between the electrodes remains constant during the electrolytic process. A feature of the invention is that inert anodes and wetted cathodes are used. An advantage of this feature is that energy savings can be realized through control of the anode-cathode distance.

Still another object of the present invention is to provide a method of alumina electrolysis whereby the generation of greenhouse gases, e.g., carbon dioxide and fluorocarbons, is eliminated. A feature of the invention is that the anodes used are inert. An advantage of this feature is that the only gas generated during the electrolysis of alumina is oxygen (O₂). An additional advantage is that costs are lowered even more due to the elimination of the carbon plant for the production of carbon anodes, and a reduced need for any emission controls.

Briefly, the invention provides an improved electrolyte for the low-temperature electrolysis of alumina (Al₂O₃), the electrolyte comprising alumina, and a mixture of aluminum fluoride (AlF₃) and potassium fluoride (KF).

The invention also provides a method for using inert anodes and wetted cathodes in the electrolytic production of aluminum comprising using the anodes and cathodes in an electrolysis process selected at a temperature selected from between 660° C. and 1000° C.

In addition, the invention provides a method for electrolyzing alumina below 1000° C., the method comprising supplying an electrolyte containing more than 35 mol % potassium fluoride (KF) and more than 30 mol % aluminum fluoride (AlF₃); injecting alumina with the electrolyte; and subjecting the electrolyte to a voltage.

BRIEF DESCRIPTION OF DRAWINGS

The invention together with the above and other objects and advantages will be best understood from the following detailed description of the preferred embodiment of the invention shown in the accompanying drawing, wherein:

FIG. 1 is a schematic diagram of the potassium fluoride-aluminum fluoride binary system, in accordance with features of the present invention;

FIG. 2 is a schematic diagram of a vertical electrode arrangement design, in accordance with features of the present invention;

FIG. 3 is a schematic diagram of an electrolysis cell for testing electrodes; and

FIG. 4 is a plot of electrolysis cell voltage in volts as a function of time for one 50-hour electrolysis run at a current of 100 A with an aluminum-bronze copper alloy inert anode and two wetted cathodes of TiB₂—C composite in a vertical arrangement, in accordance with features of the present invention.

DETAILED DESCRIPTION OF THE INVENTION

The invention provides a low temperature electrolyte system for the electrolytic production of aluminum metal (Al) that enables the use of inert anodes, wetted cathodes, and/or bi-polar electrodes, in vertical, horizontal, or other configurations. The low temperature electrolyte system is based on the aluminum fluoride (AlF₃)—potassium fluoride (KF) binary system, FIG. 1, and can include additives to change electrolyte properties.

Electrolyte Detail

The phase diagram of the AlF₃—KF system, FIG. 1, shows that the system has a much wider range of low temperature (<800° C.) liquid compositions than the aluminum fluoride (AlF₃)—sodium fluoride (NaF) system. At 700° C., the single-phase liquid region extends from about 60 mole (mol) % KF—40 mol % AlF₃ to about 40 mol % KF—60 mol % AlF₃. Because of this wide range, the bath composition in an AlF₃—KF based system is easier to control and maintain in the liquid phase in commercial low-temperature aluminum electrolysis than that of an AlF₃—NaF-based low temperature bath which has an eutectic temperature at 698° C. and is essentially a single-point composition (no line or region) of 54 mol % NaF—46 mol % AlF₃ at 700° C.

Surprisingly and unexpectedly, the inventors have found that the AlF₃—KF-based system is well-suited for electrolytic production of aluminum at temperatures lower than the operating temperatures for the AlF₃—NaF electrolyte system. The AlF₃—KF-based system has higher alumina solubility compared to the AlF₃—NaF-based system. This allows for easier control of the dissolved alumina content of the bath. The AlF₃—KF-based system has the appropriate density and interfacial energy with aluminum to permit effective separation of bath and aluminum metal product and coalescence of aluminum droplets. The AlF₃—KF-based system has adequate viscosity to allow for efficient mixing of the electrolyte resulting from convection due to rising oxygen gas bubbles from the anode during electrolysis. Viscosity is higher when solid particles such as undissolved alumina are present, and may prevent sufficient mixing of the electrolyte. Further, the higher viscosity may hinder the mobility of gas bubbles evolving from the anode, which can result in a higher cell voltage due to excessive gas bubbles present between the anode and cathode, which would increase the resistance of the cell.

In the AlF₃—KF-based electrolyte, lower bath viscosity is aided by the relatively higher alumina solubility (5 wt. % in AlF₃—KF vs. 2 wt. % in AlF₃—NaF), which allows for electrolysis operation in a liquid melt.

The inventors have also found that aluminum fluoride-potassium fluoride melt compositions with higher cryolite ratios (moles of KF to moles of AlF₃) have better ionic conductivities. Ionic conductivities in the AlF₃—KF system are improved over those in the AlF₃—NaF system. This is most likely due to the wide range of liquid compositions at lower temperatures. The inventors have found that with AlF₃—KF based electrolytes, potassium ions (K⁺), due to their larger size, do not intercalate into cathode materials (enter into the cathode substrate materials' lattices), unlike smaller sodium ions (Na⁺) in AlF₃—NaF based electrolytes at higher temperatures.

The AlF₃—KF electrolyte at 700° C. can have a KF to AlF₃ mole ratio of from about 1.0 (50 mol % AlF₃—50 mol % KF) to 1.5 (40 mol % AlF₃—60 mol % KF) and where the amount of alumina dissolved in the electrolyte is sufficient to perform electrolysis, from about 2 wt. % to 6 wt. %. This alumina solubility eliminates the need for a slurry-cell-type operation to maintain a sufficient amount of alumina dissolved in the melt.

A preferred electrolyte embodiment is a KF to AlF₃ mole ratio of about 1.3 (43 mol % AlF₃—57 mol % KF) and an alumina concentration of from about 4 wt. % to 5 wt. %. These concentrations improve the electrolysis process by lowering cell voltage. This embodiment is near the liquidus line associated with K₃AlF₆ in FIG. 1. Conductivity of the bath is strongly dependant on the K⁺ ion concentration. Thus, baths with higher KF level generally result in a lower cell voltage.

Inasmuch as aluminum metal is being produced at the cathode, the concentration of KF in the near-cathode region can be higher than in the bulk bath during electrolysis. If the bulk bath composition is too near the liquidus line, solid K₃AlF₆ can precipitate on the cathode, decreasing the effective surface area available for electrolysis and increasing cell voltage. Additionally, the precipitate can result in incomplete wetting of a wettable cathode, causing processing inefficiencies, as described infra. Thus, the preferred embodiment of the bulk electrolyte composition is given by a KF to AlF₃ mole ratio of about 1.3 rather than 1.5, which is at the liquidus line at 700° C.

Higher temperature improves electrical conductivity and increases the composition range of the liquid, so the temperature of the electrolyte can be higher than 700° C. for improved cell operation. The electrolyte can be used at temperatures as high as 1000° C. In such a case, the optimum electrolyte composition will be slightly richer in KF to maintain the optimum composition within about 2 mol % from the liquidus line, further improving the electrical conductivity. Although higher temperatures can lead to higher electrolyte conductivities and lower cell voltages, lower temperatures are less corrosive and enable the use of a larger selection of inert anode materials. The inventors found temperatures of about 700° C. to be optimal and thus one preferred embodiment of operation.

Additives can improve or alter the AlF₃—KF electrolyte system properties. One such additive can be NaF, which can be added to the electrolyte or allowed to build up in the electrolyte due to the residual sodium ion (Na⁺) level that can be present in the alumina feed to the cell, if the cell is used continually for long periods of time. This residual NaF can result from the use of sodium hydroxide (NaOH) in the Bayer process for the production of alumina feed.

An increase in NaF in the electrolyte can have detrimental effects on cell performance. At elevated levels of NaF in the electrolyte, a solid deposit can form intermittently on the cathode and cause inefficiencies in the cell, as well as increasing the impurity level of the aluminum metal product.

The inventors have found that small additions of NaF (>2 wt %) cause detrimental cell operations at both the cathode and anode. The presence of a small amount of Na⁺ cations in the bulk electrolyte is magnified in the near-cathode region during electrolysis. During electrolysis, the majority of the electrical current through the cell electrolyte is carried by the cations (Na⁺ and K⁺) because of their smaller size and greater mobility compared to the anions in the electrolyte. Because Na⁺ cations are smaller and more mobile than K⁺, Na⁺ cations tend to concentrate near the negatively-charged cathode surface. The increase in local NaF/KF ratio in the near-cathode region changes the local electrolyte composition, which decreases the alumina solubility in the region, and causes alumina and/or cryolite-type compounds to precipitate on the cathode as an intermittent grayish film. The inventors have observed this film.

The presence of this film on the cathode surface disrupts cell operation by preventing aluminum from wetting the cathode and disrupting aluminum metal coalescence. The aluminum metal which forms on the cathode tends to become dispersed in electrolyte as fine droplets of molten aluminum that are swept up by convection currents in the bath. The aluminum droplets can even come in contact with the anode, disrupting the anode surface film and accelerate the anode wear rate. Other cations, including alkali or alkaline earth cations, can also play a role as minor additives to this base electrolyte to modify the liquidus region or physical properties of the electrolyte.

In addition to the detrimental effects caused at the cathode that could also effect the anode, the presence of Na⁺ in the electrolyte can have a detrimental effect which can contribute to a higher anode wear rate. Sodium ion can cause redistribution of anion moieties in the electrolyte and alter the effect anion moieties have on anode wear. The primary oxygen-containing anion moieties in the KF—AlF₃—Al₂O₃ electrolyte are most likely oxyhexafluorodialuminate ion (Al₂OF₆ ²⁻) and dioxytetrafluorodialuminate ion (Al₂O₂F₄ ²⁻). During electrolysis, Al₂O₂F₄ ²⁻ is readily oxidized to Al₂OF₆ ²⁻ liberating oxygen gas, while Al₂OF₆ ²⁻ is not significantly oxidized. Thus, the total concentration of both oxygen-containing anions in the electrolyte at the anode surface does not change significantly. This is significant if the anode surface is an oxide film or oxygen-containing species, as it most likely is in most inert anode formulations. The driving force to dissolve the oxide film or oxygen-containing species on the anode surface is minimal because of the presence of oxygen-containing anions in the electrolyte at the anode surface. Control of the electrolyte bath composition in the AlF₃—KF system is more flexible than in the AlF₃—NaF system due to only small losses of KAlF₄ from the electrolyte melt.

In NaF—AlF₃—Al₂O₃ electrolytes the ratio Al₂OF₆ ²⁻ anions to Al₂O₂F₄ ²⁻ anions is significantly greater than in KF—AlF₃—Al₂O₃ electrolytes. During electrolysis, the primary oxidation reaction at the anode is likely the conversion of Al₂OF₆ ²⁻ to AlF₄ ⁻ liberating oxygen gas. The result is a lower number of oxygen containing species at the anode surface, and a subsequent higher driving force to dissolve the oxide film on the anode and increasing the anode wear rate. Therefore, there appears to be a limit to which NaF can be added to a KF—AlF₃—Al₂O₃ electrolyte without significantly increasing the anode wear rate. The limit is related to the concentration of Al₂O₂F₄ ²⁻ species in the melt. The inventors found this limit is less than 2 wt. % NaF. Above this concentration of NaF in the electrolyte, excessive anode wear can occur. The same effect exists for other additives such as lithium fluoride (LiF).

An electrolyte-cleansing operation can be used either in situ or ex situ of the cell, and the detrimental moiety can be removed by a variety of means, e.g., collection by zeolite-like or porous carbon structures. In the alternative, the detrimental moiety can be reduced in the electrolyte by altering upstream processing, i.e., using KOH in the aforementioned Bayer process to reduce the sodium content in the alumina feed.

Electrode Detail

Due to the lower temperature of the AlF₃—KF based electrolyte system discussed supra, the invented low temperature electrolyte system uses low-cost metal materials in the form of inert anodes and wettable cathodes. As such, commercially-available metals and metal alloys can be used as inert anodes in the instant invention. Composite materials can be used for wettable cathodes.

The use of inert anodes allows for the distance between anode and cathode to be constant during the electrolysis of alumina. This feature provides an electrically stable electrolysis environment.

In addition to inert anodes and wetted cathodes, the invented electrolyte system works works well with other electrodes, including conventional carbon anodes and carbon cathodes.

1. Anodes

The anode is comprised of a material selected from the group consisting of metals, metal alloys, metal oxides, and cermets. The alloys can be aluminum-bronze alloys, i.e., alloys that are primarily copper and have significant amount of added aluminum (1 to 20 wt. %). Commercially available aluminum-bronze alloys (including, but not limited to, Unified Numbering System (UNS) numbers C60800 to C60210, and C95200 to C95900) appear well suited for use as inert anodes. For example, alloy C63000 (specifications: 9.0 to 11.0 wt. % Al, 4.0 to 5.5 wt. % Ni, 2.0 to 4.0 wt. % Fe, 1.5 wt. % Mn, 0.30 wt. % Zn, 0.25 wt. % Si, 0.20 wt. % Sn) performed well, and thus is a preferred formulation for an inert anode.

Preferable anodes are metal monoliths which have a stable oxygen-containing film that forms during electrolysis and does not contribute significantly to the cell operating voltage. Typically, the anodes with oxide or oxygen-containing films have a polarization voltage of less than 0.5 volts (V) at a current surface density of 0.8 amperes per square centimeter (A/cm²).

Metallic anodes have other advantages which include improved electrical conductivity through the anode, improved resistance to thermal shock, and improved toughness and ductility for easier fabrication, handling, and installation.

Commercially-available copper-based alloys perform satisfactorily, particularly the aluminum-bronze copper alloys such as UNS C63000. The impurity levels of the aluminum metal product formed using UNS C63000 as the anode were 0.09 wt % Cu, 0.03 wt % Fe and <0.01 wt % Ni in a 50-hour (hr) electrolysis test (infra) at a total current of 100 A using a commercial copper alloy as the anode.

2. Cathodes

The cathode is made of a material compatible with the environs associated with alumina electrolysis. Generally, suitable material is that wetted by aluminum. Appropriate cathode substrate material includes that selected from the group consisting of metal borides, metal boride-carbon composites, metal boride-containing coatings on substrates, graphite (C), molybdenum (Mo), and tungsten (W). The metal borides include, but are not limited to, those of titanium (Ti) and zirconium (Zr). Other materials which can be wetted by aluminum can be used as cathodes.

Molten aluminum wets well the TiB₂—C composite. Wettable cathodes decrease the cathodic over potential during electrolysis, compared to non-wetted cathodes, and allow for a lower anode-to-cathode distance during electrolysis, further decreasing operating voltage. Wetted cathodes also promote coalescence of the molten aluminum product thereby improving the efficiency of the process by minimizing back reactions. The use of wetted cathodes and inert anodes is enabled by the low-temperature electrolyte and allows for the arrangement of anode and cathode in a vertical position.

A vertical arrangement allows metal that forms on the cathode to drip off the bottom of the cathode and collect at the bottom of the cell. In addition, the vertical configuration lowers the anode-cathode distance and allows for a smaller cell footprint or size, leading to lower heat input requirements. Lower heat input makes possible lower current densities which further adds to cell efficiency. In cells with horizontally-arranged arranged electrodes, a lesser anode-cathode distance aids in minimizing process inefficiencies due to fluctuations at the bath-aluminum interface resulting from magnetic fields generated in the aluminum metal pad during electrolysis.

Cathodes made of TiB₂—C composite are wetted by the aluminum at 700° C. and perform well as cathodes in the AlF₃ —KF electrolyte. Other materials wetted by aluminum will also perform well.

FIG. 2 infra serves to illustrate the concept of a cell with a vertical electrode design. The number of electrodes shown is one possible illustration and embodiment.

Electrolytic Cell Configuration

The orientation of the inert anodes and wetted cathodes in the cell can be vertical, slanted, or horizontal. A vertical design using the sequence anode 12—cathode 14—cathode 14—anode 12—cathode 14—cathode 14—anode 12 is depicted in FIG. 2 as numeral 10. In this sequence, electrolysis occurs between the anode 12 and cathode 14, but not between the two adjacent cathodes 14. Oxygen evolving during electrolysis sweeps the electrolyte to the top of the cell. The electrolyte returns to the bottom of the cell through the cathode-cathode chambers 18.

Thus, electrolyte recirculation paths are established in the spacing regions between adjacent cathodes 14. This arrangement promotes convection currents through the cell and maintains a more uniform electrolyte composition. The spacing between the chambers can be optimized for electrolyte flow and velocity, taking into account evolving oxygen gas. Many electrode arrangements are possible that include regions in the cell where electrolysis does not occur and recirculation paths are established.

The lower operating temperature of the invented AlF₃—KF electrolyte system allows for bipolar plates to be used in multi-polar cells. The cathode materials described supra can be used to coat one side of an inert anode to create a bipolar electrode for use in multipolar electrolytic cells. For example, bipolar electrodes can comprise an aluminum bronze inert anode coated with TiB₂ on a first side. At the lower operating temperature of the invented AlF₃—KF electrolyte system, TiB₂ can also be used directly as the plate material in bipolar cells. In a cell configured with bipolar plates, the electrode arrangement can be such that electrolyte recirculation paths are established.

The following example is simply to illustrate the testing and use of the new electrolyte and electrodes of the instant invention and to demonstrate their effectiveness.

FIG. 3 infra serves only to illustrate the general aspects of an electrolytic cell and the cell's components.

EXAMPLE

One electrolysis run was carried out for a period of 50 hours (hrs) at a current of 100 amperes (A). A schematic diagram of the basic form of the experimental cell is depicted in FIG. 3 as numeral 30. The cell's 30 components are contained in a sintered alumina crucible 32, which is depicted as generally cylindrical in shape. Alumina is fed into the cell 30 via a sintered alumina tube 34, which has a first end 36 protruding from the cell, and a second end 38 protruding within the confines 40 of the cell. The temperature is monitored with a platinum (Pt)—Pt-10% rhodium (Rh) thermocouple 42 housed in a closed-end alumina tube 44. A first end 46 of the thermocouple 42 terminates with pair of electrical leads 48, while a second end 50 of the thermocouple 42, swathed in the alumina tube 44, is immersed in the electrolyte 52 (represented by the dashed lines).

A stainless steel rod 54 extending generally parallel with the longitudinal axis of the crucible, serves as a current lead for the anode 56. Generally, the anode is placed in a concentric position within the cell for optimized results. The faces of the two cathodes 58 are parallel to the faces of the anode 56. The cathodes 58 have stainless steel current leads 60. Sintered alumina sheaths 62 protect and electrically insulate the stainless steel rod 54, and the stainless steel current leads 60. The aluminum fluoride-potassium fluoride melt 52 is contained within the cell 30, and typically confined at one end of the cell via gravity. The stainless steel current leads 60, the alumina feeding tube 34, and the thermocouple 42 relative positions are secured by holes in the top of the cell, all of which, as mentioned supra, extend generally parallel to the longitudinal axis of the crucible 32.

Runs were carried out under an argon (Ar) atmosphere. The argon gas flow was kept at 1.13 Liters per minute (L/min). An oxygen sensor was mounted on the outlet gas path to measure the amount of oxygen generated on the alloy anodes.

The basic cell design (FIG. 3) as used for the 50-hr, 100 A run, employed a parallel vertical plate arrangement. Three plate electrodes were employed comprising a central anode plate between two cathode plates. The size of each electrode plate was approximately 133 millimeters (mm) wide, 85 mm high, and 12 mm thick. The anode was made of aluminum-bronze (alloy C63000, composition specifications given supra), and the cathodes were made of TiB₂—C composite. The anode-cathode distance was 2.3 cm. The initial electrolyte composition was 50 wt. % AlF₃, 45 wt. % KF, and 5 wt. % Al₂O₃. Alumina was fed continuously to the cell during electrolysis. The electrolysis test was performed at 700° C. and the anode current density was maintained at 0.44 A/cm² for the duration of the 50-hr test.

FIG. 4 depicts a plot of electrolysis cell voltage in volts as a function of time for this run. The voltage remains fairly constant at a current of 100 A for a period of 50 hr. A significant amount of aluminum product corresponding to a current efficiency of 85% was recovered at the conclusion of the test run. Subsequent analysis indicated impurity levels of 0.09 wt. % Cu, 0.03 wt. % Fe and <0.01 wt % Ni. Anode wear was not detected, although a 200-300 micrometer (μm) thick oxide film was found on the surface of the anode.

While the invention has been described with reference to details of the illustrated embodiment, these details are not intended to limit the scope of the invention as defined in the appended claims. 

1. An improved electrolyte for the electrolysis of alumina (Al₂O₃), the electrolyte comprising a mixture of aluminum fluoride (AlF₃) and potassium fluoride (KF).
 2. The electrolyte recited in claim 1 wherein the aluminum fluoride (AlF₃) is present in a molar ratio with potassium fluoride (KF) greater than 1:1.
 3. The electrolyte recited in claim 1, the electrolyte further comprising from about 2 to 6 wt. % of aluminum oxide (alumina/Al₂O₃).
 4. The electrolyte as recited in claim 1 wherein the concentrations of the electrolyte's components remain constant during electrolysis.
 5. The electrolyte as recited in claim 1 where the electrolyte is used to electrolyze the alumina to aluminum at from about 660° C. to 1000° C.
 6. The electrolyte as recited in claim 3 wherein the electrolyte remains liquid during electrolysis.
 7. The electrolyte as recited in claim 6 wherein inert anodes and wettable cathodes can be used with the electrolyte.
 8. A method for using inert anodes and wettable cathodes in the electrolytic production of aluminum comprising using the anodes and cathodes in an electrolysis process at a temperature from between 660° C. and 1000° C.
 9. The method as recited in claim 8 wherein the anode is comprised of a material selected from the group consisting of metals, metal alloys, metal oxides, and cermets.
 10. The method as recited in claim 8 wherein the alloys are copper alloys (aluminum-bronze) and are from about 1 wt. % to 20 wt. % aluminum (Al).
 11. The method as recited in claim 8 wherein the cathode is made of a material selected from the group consisting of metal borides, metal boride-carbon composites, metal boride-containing coatings on substrates, graphite, molybdenum, and tungsten.
 12. The method as recited in claim 8 where the anode contains an oxygen-containing film.
 13. The method as recited in claim 12 wherein the oxygen containing film is formed during the electrolysis process.
 14. The method as recited in claim 11 wherein the material coats one side of the inert anode to create a bipolar electrode for use in multipolar electrolytic cells.
 15. The method as recited in claim 8 wherein the distance between the anode and cathode remains constant.
 16. The method as recited in claim 8 wherein the electrodes can be arranged in a vertical configuration.
 17. The method as recited in claim 8 wherein the electrodes can be arranged in a slanted configuration.
 18. The method as recited in claim 8 wherein O₂ is the only gas generated by electrolysis.
 19. The method as recited in claim 16 wherein the vertical configuration of the cell creates electrolyte recirculation pathways.
 20. A method for electrolyzing alumina below 1000° C., the method comprising: a) supplying an electrolyte containing more than 35 mol % potassium fluoride (KF) and more than 30 mol % aluminum fluoride (AlF₃); b) injecting alumina with the electrolyte; and c) subjecting the electrolyte to a voltage. 